US2932318A - Naphtha air sweetening - Google Patents

Naphtha air sweetening Download PDF

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US2932318A
US2932318A US51499355A US2932318A US 2932318 A US2932318 A US 2932318A US 51499355 A US51499355 A US 51499355A US 2932318 A US2932318 A US 2932318A
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naphtha
tank
air
sweetening
level
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George W Ostberg
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G27/00—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation
    • C10G27/04—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/8593—Systems
    • Y10T137/86348—Tank with internally extending flow guide, pipe or conduit
    • Y10T137/86372—Inlet internally extending

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  • the present invention relates-to a process and apparatus for sweetening naphtha compositions. More spe oifically, in accordance with the present invention sour gasoline stocks are sweetened by contact with air in a storage tank equipped with baffling means whereby maximum residence time of control between incoming air and naphtha is realized to produce a completely air sweetened naphtha. Y I
  • sour naphtha is generally sweetened in storage tanks under conditions to obtain thenecessary residence time to convert mercaptans to disulfides.
  • This residence time of the order of 24 to 96 hours, depending upon the characteristics of the crude, has been obtained by passing air-treated naphtha from amixingzone to a storage tank equipped with two inlet nozzles. One nozzle is located at ground level and the second about 10 feet above the lower nozzle. When the tank is empty or nearly so, the lower inlet nozzle is used for'filling.
  • the naphtha is passed in at production rate, i.e., the, rate at which it is produced at the processing unit.
  • the second or upper nozzle of the tank is replaced by a suitable bafile such as a plate or box bafllc.
  • the bafile is installed with sufficient clearance from the tank. floor so that with normal flow input, the level within the bafiled section is about 3 to 6 inches higher than the level on the storage side.
  • the bafiie extends upward for approximately one third to one half of the height of the tank.
  • Figure I is a schematic diagram of a process for sweetening sour naphtha.
  • Figure Ia is a partial top sectional view of naphtha storage tank 20 of Figure I.
  • Figure Ib is a partial top sectional view of a modification of the storage tank shown in Figure la.
  • FIG II is a partial side sectional view of a naphtha storage tank wherein the bafile is pipe 30.
  • Figure III is a plan view of the storage tank in Figure II with the interior baffie shown in dotted lines.
  • Figure IV is a partial side sectional view of a modification of the storage tank shown in Figures II wd III.
  • the sour naphtha is preferably given a preliminary caustic wash in vessel 2 to remove hydrogen sulfide, which would be converted to free sulfur in the subsequent air treating step.
  • the naphthas to be sweetened by this process may be identified by reference to the mercaptan content of the stock.
  • the sweetening process is particularly applicable to those gasolines, having a copper number ranging from about 1 or less, to 15.
  • such gasolines may also constitute gasolines obtained from prior sweetening operations or from relatively low sulfur crude oils, and particularly from gasolines derived from thermal or catalytic cracking operations.
  • Caustic soda employed for the caustic wash may be introduced through line 4 for mixture with the sour naphtha in vessel 2, which may be an orifice mixer. About 1-10 volumes of 530% caustic may be employed.
  • the process is preferably operated continuously, but throughput must be controlled so that the hold-up time in zone 26 is sutficient to complete sweetening.
  • the naphtha admixed with air is conducted to bathed storage'vessel 20.
  • This vessel is-a conventional storage tank adapted for storing volatile and inflammable hydrocarbons but, in accordance with the present invention, also equipped with bathe 22.
  • the vessel is of sufficient size for 4 days production hold-up, for example 40' diameter by 36' height.
  • Battle 22 may be of plate (Figure Ta) or box ( Figure lb) design and its lower portion afiords a clearance or underpass of about 5 to square inches, that is,
  • the bathe is installed with sutficient clearance from the tank floor so that with normal flow input of 1600-4000 barrels per stream day, the level within the bafile section is' 3-6 inches higher than the level on the storage side.
  • the bafile extends upwardly approximately one half the height of the tank. In one embodiment, it is welded to the tank wall.
  • the air-mixed naphtha is passed into tank through line 24 and nozzle 26.
  • the level within the bathed section is some 3-6 inches higher than the level on the storage side, the naphtha passing under the bafile.
  • the naphtha level in the tankage reaches the top of bathe 22, 95-100% of the flow is upward and the remainder through the underclearance in the bottom portion of the tank.
  • This results in part from the warmer temperature of the incoming naphtha which may be 70 to 100 F. while the bottom portion approaches ambient temperature, say 50' to 80 F., and also by the higher resistance to flow underneath the battle.
  • the tank may be filled to a level substantially above the top of the bathe without loss of effective residence time.
  • the aged product now fully air-sweetened, is withdrawn from tanks 20 through outlet nozzle 28 and is further processed in a manner not forming a part of the present invention. Thus, it may be water-washed if desired, or passed directly to storage. Similarly, tank 20 may be further provided with vents and outlets towithdraw air separated from the naphtha.
  • FIG. 1 Another embodiment of the present invention is shown in .Eigure Ii.
  • the bafiling effect is provided by a vertical pipe 30 coupled to the tank inlet nozzle 32.
  • Pipe 30 is about 10-20 feet in length and 12-16 inches in diameter, and the corresponding nozzle may be 4-6 inches in diameter.
  • slot 34 Opposite the inlet nozzle in pipe30 is slot 34, having an area of 5-10 square inches, providing for bottom flow of naphtha into the tank, as in the case of the battle previously described.
  • a swingor other type check valve maybe, used instead of bottom slot or orifice 34.
  • Such arrangement is shown in Figure IV.
  • this alternate pipe 30 may be installed in a naphtha storage tank 40 feet in diameter and 36 feet high.
  • Standpipe 30 is 12 inches in diameter and stands 15- feet high.
  • Slot 34 measures 1 inch by 5 inches, and the'dserverrential bead through slot 34 is about 4 inches.
  • the naphtha flows upwardly through standpipe 30 and passes-into the tank through. its upper openings 36.
  • the relationship of standpipe 30' to tank 20 is clearly seen in Figure III.
  • T he standpipe arrangement has the advantage of minimizing welding in the tank, cheaper and simpler construction, and easier installation.
  • the 12" pipe with a 4" connection may readily be carried into a tank of? say 40 diameter and '36 height through the standard 24" manhole.
  • the larger size standpipe, say 16" size with 6" connection is used for larger tanks handling large naphtha rates, and can be entered through the standard 28" manhead on these tanks.
  • a naphtha storage tank in combination. a tank, conduit inlet means in the lower portion of said. tank adapted to conduct vaporizable liquids into said tank, a' vertical bathe attached to the side wall of said tank to form a flow space between said bafile and said side wall which communicates with said inlet means, said bafile being positioned above the floor. of said tank and extending upwardly to /2 the height of said tank, said baffle additionally being positioned close to said inlet. means and extending. downwardly to form with the floor of said tank an opening having substantially smaller cross" section than said inlet means, and conduit means in the lower portion of said tank adapted to withdraw said liquid, said last named conduit means being further removed from said bathe than said conduit inlet means.
  • baflle is a box baffle.
  • conduit inlet means in the lower portion of said tank adapted to conduct vaporizable, liquids
  • a vertical pipe positioned on the floor of said tank and in communication with said inlet means, said pipe extending for a distance of about /s- /z the height of said tank and the upper portion of said pipe being in open communication with said tank, outlet means in the lower portion of said pipe, said outlet means being of substantially smaller cross section than said inlet means, and conduit means in the lower portion of said tank adapted to withdraw said liquid, said last-named means being substantially further removed from said pipe than said inlet means,

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Description

April 12, 1960 G. w. OSTBERG 2,932,313
V NAPI-ITHA AIR SWEETENING Filed June 15, 1955 2 Sheets-Sheet 1 FIGURE I0 FIGURE Ib FIGURE JI George W. Ostberg Inventor By Attorney April 2, 1960 G. w. QSTBERG 2,932,318
NAPHTHA AIR SWEETENING Filed June 13, 1955 2 Sheets-Sheet 2 INHIBITOR AIR I STORLkGE SETTLER, MIXER TAN I lz l} I6 I4 20 MIXER '2 SPENT I CAUSTIC I cAusTIc I 28 SOUR FIGURE I NAPHTHA NAPHTHA TANK -20 :36 7 a i I I I AL; I a -II-I 34 FIGURE 111.
FIGURE JI George W Qsfberg Inventor WW 7Attorney United States Patent NAPHTHA AIR SWEETENING George W. Ostberg, Roselle Park, NJ., assignor to Esso Research and Engineering Company, a corporation of Delaware Application June 13, 1955, Serial No. 514,993
8 Claims. (Cl. 137-592) The present invention relates-to a process and apparatus for sweetening naphtha compositions. More spe oifically, in accordance with the present invention sour gasoline stocks are sweetened by contact with air in a storage tank equipped with baffling means whereby maximum residence time of control between incoming air and naphtha is realized to produce a completely air sweetened naphtha. Y I
The removal of undesired sulfur compounds from petroleum products is a perennial problem in the petroleum refining industry. While there have been many suggestions made as to processes for removing undesired sulfur compounds, the desire for simplified sulfur removal processes remains. Again new problems are encountered in the processing of novel feed stocks or unusual blends of stocks.
comparatively recently it has been discovered that certain stocks are susceptible to what is known as air sweetening. For example, certain gasolines during simple storage under conditions to expose the gasolines to oxygen will undergo a process in which mercaptans are converted to disulfides. This conversion of sulfur compounds from mercaptans to disulfides is called sweetening by virtue of the fact that the disulfides, unlike the mercaptans, are not malodorous. The basic simplicity of the air sweetening process holds great promise as a finishing procedure for stocks susceptible to this treatment in order to provide the last incremental improvement in sweetening which is often required. The present invention is concerned with animprovcment in air sweetening techniques providing for increased rates of sweetening of those stocks which respond to air sweetening. It is a particular feature of the process that it has been found to be of particular application to the sweetening of blends of cracked gasolines with virgin gasolines, since virgin gasolines are normally unresponsive to air sweetening.
1 In commercialinstallations, sour naphtha is generally sweetened in storage tanks under conditions to obtain thenecessary residence time to convert mercaptans to disulfides. This residence time, of the order of 24 to 96 hours, depending upon the characteristics of the crude, has been obtained by passing air-treated naphtha from amixingzone to a storage tank equipped with two inlet nozzles. One nozzle is located at ground level and the second about 10 feet above the lower nozzle. When the tank is empty or nearly so, the lower inlet nozzle is used for'filling. The naphtha is passed in at production rate, i.e., the, rate at which it is produced at the processing unit. When the naphtha level reaches the upper nozzle, the lower connection is shut off and the upper one is opened. This allows. the incoming naphtha, which is usually warmer than the naphtha in tankage, to remain as'the top stratumof the naphtha. Since the naphtha is withdrawn through a nozzle or port, also situated at ground level, the naphtha that is withdrawn from the bottom is that which has remained in the tank for the longest period. The arrangement described has been found not to be completely satisfactory. In the first place, it requires 2,9323% Patented Apr. 12, 1960 2 constant operating attention to insure proper closure and opening of valves, depending upon the level of the airtreated naphtha within the tank. Also, there is a potential safety hazard of naphtha discharging through the elevated nozzle above the liquid level of the naphtha. Furthermore, when the level of'the naphtha is appr e; ciably above the topinozzle, maximum residence time is not attained as the horizontally entering naphtha mixes and circulates with naphtha partially aged in the'tanks.
It is, therefore, the principal object of the present invention to set forth a naphtha sweetening tank specifically adapted to overcome the above mentioned disadvantages in commercial installations.
It is a further purpose and object of the present invention to set forth a tank arrangement aifording a maximum of residence time, elimination of operating attention, and elimination of a potential safety hazard.
Other and further objects and advantages of the present invention will become apparent hereinafter.
In accordance with the present invention the second or upper nozzle of the tank is replaced by a suitable bafile such as a plate or box bafllc. The bafile is installed with sufficient clearance from the tank. floor so that with normal flow input, the level within the bafiled section is about 3 to 6 inches higher than the level on the storage side. The bafiie extends upward for approximately one third to one half of the height of the tank. When the naphtha level in tankage reaches the top of the baflle -l00% of the flow is upward, and the remainder is through the underclearance to the bottom portion of the tank. This division is affected by both the warmer temperature of the incoming naphtha and the higher resistance to flow underneath the bafiie. Consequently, the incoming naphtha is diverted vertically to the top of the naphtha volume, and maximum residence time for the sweetening and aging is obtained.
The present invention will be more clearly understood when read in conjunction with the drawings which represent schematically preferred embodiments thereof.
In the drawings:
Figure I is a schematic diagram of a process for sweetening sour naphtha.
Figure Ia is a partial top sectional view of naphtha storage tank 20 of Figure I.
Figure Ib is a partial top sectional view of a modification of the storage tank shown in Figure la.
Figure II is a partial side sectional view of a naphtha storage tank wherein the bafile is pipe 30.
Figure III is a plan view of the storage tank in Figure II with the interior baffie shown in dotted lines.
Figure IV is a partial side sectional view of a modification of the storage tank shown in Figures II wd III.
Turning now to Figure I, the sour naphtha is preferably given a preliminary caustic wash in vessel 2 to remove hydrogen sulfide, which would be converted to free sulfur in the subsequent air treating step. The naphthas to be sweetened by this process may be identified by reference to the mercaptan content of the stock. As indicated by the copper number of the gasoline, the sweetening process is particularly applicable to those gasolines, having a copper number ranging from about 1 or less, to 15. As will be understood, such gasolines may also constitute gasolines obtained from prior sweetening operations or from relatively low sulfur crude oils, and particularly from gasolines derived from thermal or catalytic cracking operations.
Caustic soda employed for the caustic wash may be introduced through line 4 for mixture with the sour naphtha in vessel 2, which may be an orifice mixer. About 1-10 volumes of 530% caustic may be employed.
It has also been found desirable to add an antioxidant inhibitor to the naphtha prior to or during the subsequent air-sweetening process. Of particular effectiveness are the phenylene diamines, inparticular, the N,N" .di-alkyl- The caustic-washed naphtha is then passed to an air'-' mixing zone 16. Air may be introduced throughlin'e, 18
by means of a compressed air line'or 'the 'lik'e'; The air injected should not be less than about 0.05 standard cubic foot per copper number per barrel ofnaph'tha treated; Thus for a gasoline of 10 copper number, 0.5's.c.f. of
air per barrelis about the minimum requirement, but
about 1.5 s.c.f. is preferred to speed up the sweetening rate.
The process is preferably operated continuously, but throughput must be controlled so that the hold-up time in zone 26 is sutficient to complete sweetening.
In accordance with the present invention, the naphtha admixed with air is conducted to bathed storage'vessel 20. This vessel is-a conventional storage tank adapted for storing volatile and inflammable hydrocarbons but, in accordance with the present invention, also equipped with bathe 22. The vessel is of sufficient size for 4 days production hold-up, for example 40' diameter by 36' height. Battle 22 may be of plate (Figure Ta) or box (Figure lb) design and its lower portion afiords a clearance or underpass of about 5 to square inches, that is,
the bathe is installed with sutficient clearance from the tank floor so that with normal flow input of 1600-4000 barrels per stream day, the level within the bafile section is' 3-6 inches higher than the level on the storage side. The bafile extends upwardly approximately one half the height of the tank. In one embodiment, it is welded to the tank wall.
The air-mixed naphtha is passed into tank through line 24 and nozzle 26. As indicated previously, initially the level within the bathed section is some 3-6 inches higher than the level on the storage side, the naphtha passing under the bafile. At this stage, it is generally not desirable to withdraw naphtha from outlet nozzle 28, due to incomplete ageing. When the naphtha level in the tankage reaches the top of bathe 22, 95-100% of the flow is upward and the remainder through the underclearance in the bottom portion of the tank. This results in part from the warmer temperature of the incoming naphtha which may be 70 to 100 F. while the bottom portion approaches ambient temperature, say 50' to 80 F., and also by the higher resistance to flow underneath the battle. Thus the incoming naphtha is diverted vertically to the top of the naphtha volume and the maximum residence time for ageing is obtained. The tank may be filled to a level substantially above the top of the bathe without loss of effective residence time.
After a holdmp period of 24 to 96 hours, the aged product, now fully air-sweetened, is withdrawn from tanks 20 through outlet nozzle 28 and is further processed in a manner not forming a part of the present invention. Thus, it may be water-washed if desired, or passed directly to storage. Similarly, tank 20 may be further provided with vents and outlets towithdraw air separated from the naphtha.
Though the process and construction of the present invention find their immediate utility in the air sweetening of naphtha, it is evident that they find utility inother applications where a maximum of residence time of a liquid in a tank, for aging 'or' other effect, is desired. The advantages of the present invention over present installations and processes include the elimination of operating attention to the tank in that there are no valves to openor close, depending upon the' level within'the' tank; the elimination of the -potential safety hazard of naphtha discharging through an elevated nozzle above the liquid level of the naphtha; and the full effectiveness of the baffie installation at all levels above the top of the battle. In prior arrangements, maximum residence time could not be realized when the naphtha level was appreciably above the top nozzle.
Another embodiment of the present invention is shown in .Eigure Ii. The bafiling effect is provided by a vertical pipe 30 coupled to the tank inlet nozzle 32. Pipe 30 is about 10-20 feet in length and 12-16 inches in diameter, and the corresponding nozzle may be 4-6 inches in diameter. Opposite the inlet nozzle in pipe30 is slot 34, having an area of 5-10 square inches, providing for bottom flow of naphtha into the tank, as in the case of the battle previously described. If desired, a swingor other type check valve maybe, used instead of bottom slot or orifice 34. Such arrangement is shown in Figure IV.
In a typical tank employing this alternate pipe 30 may be installed in a naphtha storage tank 40 feet in diameter and 36 feet high. Standpipe 30 is 12 inches in diameter and stands 15- feet high. Slot 34 measures 1 inch by 5 inches, and the'diilerential bead through slot 34 is about 4 inches. The naphtha flows upwardly through standpipe 30 and passes-into the tank through. its upper openings 36. The relationship of standpipe 30' to tank 20 is clearly seen inFigure III.
T he standpipe arrangement has the advantage of minimizing welding in the tank, cheaper and simpler construction, and easier installation. The 12" pipe with a 4" connection may readily be carried into a tank of? say 40 diameter and '36 height through the standard 24" manhole. The larger size standpipe, say 16" size with 6" connection is used for larger tanks handling large naphtha rates, and can be entered through the standard 28" manhead on these tanks.
What is claimed is:
1. 'In a naphtha storage tank in combination. a tank, conduit inlet means in the lower portion of said. tank adapted to conduct vaporizable liquids into said tank, a' vertical bathe attached to the side wall of said tank to form a flow space between said bafile and said side wall which communicates with said inlet means, said bafile being positioned above the floor. of said tank and extending upwardly to /2 the height of said tank, said baffle additionally being positioned close to said inlet. means and extending. downwardly to form with the floor of said tank an opening having substantially smaller cross" section than said inlet means, and conduit means in the lower portion of said tank adapted to withdraw said liquid, said last named conduit means being further removed from said bathe than said conduit inlet means.
2. The apparatus of claim 1 wherein said battle is a plate baffle.
3. The apparatus of claim 1 wherein said baflle is a box baffle.
4. The apparatus of claim 1' wherein said inlet means is a nozzle.
5. In a naphtha storage tank in combination a tank, conduit inlet means in the lower portion of said tank adapted to conduct vaporizable, liquids, a vertical pipe positioned on the floor of said tank and in communication with said inlet means, said pipe extending for a distance of about /s- /z the height of said tank and the upper portion of said pipe being in open communication with said tank, outlet means in the lower portion of said pipe, said outlet means being of substantially smaller cross section than said inlet means, and conduit means in the lower portion of said tank adapted to withdraw said liquid, said last-named means being substantially further removed from said pipe than said inlet means,
6. The apparatus of claim 5 wherein said outlet means from said pipe is substantially opposite said inlet means.
References Cited in the file of patent UNITED STATES PATENTS 357,793 Smith Feb. 15, 1887 1,212,574 Shipp Jan. 16, 1917 1,635,414
Hirst July 12, 1927 6 Schnetzler Oct. 28, 1930 Waechter Nov. 23, 1937 Poirier July 6, 1948 Temperly May 6, 1952 Davies Mar. 10, 1953 Mackinnon Feb. 15, 1955v FOREIGN PATENTS Great Britain Aug. 22, 1907 Great Britain Sept. 21, 1907
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WO2003086884A1 (en) * 2002-04-11 2003-10-23 Mobius Technologies, Inc. Surge tank
US20030227819A1 (en) * 2002-04-11 2003-12-11 Mobius Technologies, Inc., A California Corporation Control system and method for continuous mixing of slurry with removal of entrained bubbles
US20030227817A1 (en) * 2002-04-11 2003-12-11 Mobius Technologies, Inc., A California Corporation Mixer
US20030227818A1 (en) * 2002-04-11 2003-12-11 Mobius Technologies, Inc. A California Corporation Process and apparatus for continuous mixing of slurry with removal of entrained bubbles
US20030233937A1 (en) * 2002-04-11 2003-12-25 Mobius Technologies, Inc., A California Corporation Apparatus and method for continuously removing air from a mixture of ground polyurethane particles and a polyol liquid

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US1779918A (en) * 1927-03-10 1930-10-28 Standard Oil Co Apparatus for distilling hydrocarbon cils
US2099914A (en) * 1936-05-13 1937-11-23 Link Belt Co Method of and apparatus for influent supply
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US2595731A (en) * 1944-11-29 1952-05-06 Walmsleys Bury Ltd Liquid level control means
US2630822A (en) * 1947-05-29 1953-03-10 Parker Appliance Co Valve means for controlling the filling and draining of tanks
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US357793A (en) * 1887-02-15 John geoege smith
GB190718938A (en) * 1907-08-22 1908-08-20 William Richard Harriss Improvements in or relating to Tanks or Cisterns for Hot Water Circulation-systems or the like.
GB190721022A (en) * 1907-09-21 1908-03-26 Georg Schiessl Improvements in Apparatus for Distributing Liquids
US1212574A (en) * 1916-07-25 1917-01-16 Clarence C Shipp Automatic radiator-valve and humidifier.
US1635414A (en) * 1926-06-12 1927-07-12 Frederick W Hirst Flow regulator
US1779918A (en) * 1927-03-10 1930-10-28 Standard Oil Co Apparatus for distilling hydrocarbon cils
US2099914A (en) * 1936-05-13 1937-11-23 Link Belt Co Method of and apparatus for influent supply
US2444668A (en) * 1943-03-06 1948-07-06 Ernest A Poirier Method of and apparatus for providing a response to the consistency of papermaking stock
US2595731A (en) * 1944-11-29 1952-05-06 Walmsleys Bury Ltd Liquid level control means
US2630822A (en) * 1947-05-29 1953-03-10 Parker Appliance Co Valve means for controlling the filling and draining of tanks
US2702280A (en) * 1947-06-26 1955-02-15 Allied Chem & Dye Corp Method of mixing gas-and foamproducing liquids

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003086884A1 (en) * 2002-04-11 2003-10-23 Mobius Technologies, Inc. Surge tank
US20030227819A1 (en) * 2002-04-11 2003-12-11 Mobius Technologies, Inc., A California Corporation Control system and method for continuous mixing of slurry with removal of entrained bubbles
US20030227817A1 (en) * 2002-04-11 2003-12-11 Mobius Technologies, Inc., A California Corporation Mixer
US20030227818A1 (en) * 2002-04-11 2003-12-11 Mobius Technologies, Inc. A California Corporation Process and apparatus for continuous mixing of slurry with removal of entrained bubbles
US20030233937A1 (en) * 2002-04-11 2003-12-25 Mobius Technologies, Inc., A California Corporation Apparatus and method for continuously removing air from a mixture of ground polyurethane particles and a polyol liquid
US20040020540A1 (en) * 2002-04-11 2004-02-05 Mobius Technologies, Inc., A California Corporation Surge tank
US6860289B2 (en) 2002-04-11 2005-03-01 Robert Donald Villwock Surge tank
US6994464B2 (en) 2002-04-11 2006-02-07 Mobius Technologies, Inc Control system and method for continuous mixing of slurry with removal of entrained bubbles
US7029162B2 (en) 2002-04-11 2006-04-18 Mobius Technologies, Inc. Process and apparatus for continuous mixing of slurry with removal of entrained bubbles
US20060104156A1 (en) * 2002-04-11 2006-05-18 Mobius Technologies, Inc., A California Corporation Process and apparatus for continuous mixing of slurry with removal of entrained bubbles

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